CN1203890A - Reduction of Nox emissions in glass melting furnace - Google Patents
Reduction of Nox emissions in glass melting furnace Download PDFInfo
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- CN1203890A CN1203890A CN98107902A CN98107902A CN1203890A CN 1203890 A CN1203890 A CN 1203890A CN 98107902 A CN98107902 A CN 98107902A CN 98107902 A CN98107902 A CN 98107902A CN 1203890 A CN1203890 A CN 1203890A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/50—Glass production, e.g. reusing waste heat during processing or shaping
Abstract
The present invention provides a method of controlling NOx emissions from a glass melting process in which combustion fuel produces exhaust gas in a melting furnace including NOx compounds. Furnace exhaust gas passes from the melting furnace through a regenerator to a zone downstream from the regenerator. Ammonia is injected into the furnace exhaust gas at the downstream zone while the furnace exhaust gas is within a desired temperature range to reduce the amount of NOx compounds. Additional gas is introduced into the furnace exhaust gas whenever the furnace exhaust gas has a temperature which is outside the desired temperature range at the downstream zone so as to modify the furnace exhaust gas temperature such that the furnace exhaust gas is within the desired temperature range when furnace exhaust gas reaches to the downstream zone.
Description
The present invention relates to reduce the NO that produces in the large glass melting furnaces by control kiln spent air temperture
xDischarge.
For the temperature of fusion of requirement is provided by direct heating, extensive molten glass a large amount of fuel that need in melting furnaces, burn.In order to ensure fuel perfect combustion in kiln, especially in service at the sheet glass melting furnaces, in order to ensure the oxidizing condition in the kiln, usually fuel (being generally Sweet natural gas or oil fuel) is mixed with excess air, promptly air capacity surpasses the theoretical requirement of perfect combustion.This combustion conditions has caused the oxidation of nitrogen in the combustion air, forms NO
x
NO
xBe NO and/or NO
2Abbreviation.Under the hot conditions of glass melter, the nitrogen oxide of formation mainly is to contain small amount of N O
2NO, but after the exhaust gas emission that contains NO was in the atmosphere, most of NO changed NO into
2, NO
2Be a kind of main air pollutant, it is generally acknowledged in the chemical process that acid mist forms just to relate to this material.Therefore, the Combustion Source of large volume as glass melter, is subjected to seriously limiting the influence of the government regulations of its operation easily.
United States Patent (USP) 3,900,554 at Lyon has proposed a kind of on-catalytic method that optionally NO is reduced into the nitrogen G﹠W by inject ammonia in exhaust flow.In the United States Patent (USP) 4,328,020 of Hughes, proposed in the glass melter exhaust flow, can make in this way.This patent proposes, and the waste gas of discharging in kiln can carry out NO in 870～1090 ℃ of scopes the time (being 700～1090 ℃ when containing hydrogen in the ammonia) effectively
xReduction, and such temperature condition can be present in the flue or in flue in the most of the time of each heating period of glass melter and produce, said flue connects the firsts and seconds regenerator of melting furnaces heat recovery system.This patent also proposes, as long as the kiln spent air temperture that passes through flue just stops the injection of ammonia outside this preferred operating range.Though this method can be removed most of NO from glass melter waste gas
x, but because when spent air temperture is improper, the efficient of ammonia reduction technique is low in the selection part-time of each heating period of melting furnaces, has reduced its general effect.
In order to prolong the effective run time of ammonia injected system, people's such as Krumwiede United States Patent (USP) 4,372,770 have proposed a kind of glass melter, wherein inject extra fuel, and in the select time in the glass melting process, when kiln waste gas enters the one-level regenerator and the burning of the excessive oxygen in the waste gas, thereby improve the kiln spent air temperture, make its effective NO at the ammonia injection method
xReduce in the desired temperature range.
Though the system of these types is used for reductive NO
xDischarge, but in the heating period of glass melter, still have and can not use ammonia injected system reductive NO
xIn the time of discharge.
The layout that a kind of glass melter is preferably arranged, the use and the more effective use thereof that can increase the ammonia injected system are with further minimizing NO
xDischarge.
The invention provides the NO that a kind of feed glass melting furnaces are discharged
xMethod, wherein fuel has produced and has contained NO in melting furnaces
xThe waste gas of compound.Arrive the downstream area of regenerator by regenerator from the kiln waste gas of melting furnaces.When kiln waste gas is in the ideal temperature range, in this downstream area, ammonia is injected kiln waste gas to reduce NO
xThe content of mixture.When the kiln spent air temperture at said downstream area place exceeds the ideal temperature range, when said downstream area flows, to kiln waste gas, add extra gas to adjust the kiln spent air temperture at kiln waste gas from regenerator, make kiln waste gas when arriving said downstream area in the ideal temperature range.In a particular of the present invention, said extra gas is the waste gas from excess air burner, in certain temperature said waste gas is injected kiln waste gas, make mixing temperature at the kiln waste gas at said downstream area place and injecting gas at about 870～1090 ℃.
The present invention also provides a kind of kiln of molten glass, and a melting chamber that is interconnected and regenerator are arranged, and feasible waste gas from melting chamber enters and arrive by regenerator the downstream area of regenerator.The ammonia injector is positioned at said downstream area, is used for when the kiln waste gas that passes through downstream area is in predetermined temperature range, injects ammonia with reductive NO in kiln waste gas
xCompound.Air injector to be to introduce gas in the kiln waste gas of preset temperature between regenerator and said downstream area, makes mixing temperature at the kiln waste gas at said downstream area place and injecting gas in predetermined temperature range.In a particular of the present invention, said air injector comprises an excess air burner at least.
Fig. 1 is sheet glass melting furnaces pass through the regenerator system along the longitudinal section a side-view.Said regenerator comprises one-level regenerator and secondary regenerator and the ammonia injector between two regenerator.
Fig. 2 is the sectional view of the glass melter of Fig. 1 along the 2-2 line of Fig. 1.
Fig. 3 be amplify along the spout of regenerator and the cross-sectional view on its top.
This paper describes the present invention with reference to typical sheet glass melting furnaces, for example this paper United States Patent (USP) 4,372,770 glass melters that proposed incorporated by reference.But principle of the present invention can be applied to satisfy any glass melter of identical or conditions of similarity.
Fig. 1 and 2 represents to have the classic flat-plate glass melter 10 of a melting chamber 12.Glass batch feeds the extension 16 of the inlet of these kilns from feeding hopper 14, and sinks in the molten glass bath 18 that is included in the melting chamber 12.Kiln 10 is horizontal flame heat accumulating types of knowing, and wherein melting chamber 12 sides are a pair of one- level regenerator 20 and 22 with same structure.Each regenerator comprises a refractory brick shell 24, is a regenerator piled bricks that allows air and waste gas to constitute from the refractory brick by trellis that wherein passes through in the shell.Each regenerator 20 links to each other with melting chamber 12 by a plurality of spouts 28 of arranging along the sidewall spacers of melting chamber 12 with 22.Each spout 28 1 end stretches into the inside of melting chamber 12, and the other end links to each other with the pressure space 30 of piled bricks 26 tops of one-level regenerator.It below the piled bricks 26 in each regenerator the allocation space 32 that an end communicates with flue 34.In the embodiment depicted in fig. 1, flue 34 is connected to secondary regenerator 36, and secondary regenerator 36 can comprise one-level grid piled bricks 38 and secondary grid piled bricks 40.Cross reversing mechanism 42 from the exhaust flow of secondary regenerator, enter chimney 44 then.
Periodically to the air-flow by kiln 10 commutate (for example per approximately 10 minutes commutation once).In the operational mode in the accompanying drawings, air-flow flows (as shown in Figure 2) from left to right, and the combustion air of wherein coming in enters by the regenerator 20 in left side, and the waste gas of melting chamber 12 is discharged by the regenerator 22 on right side.The combustion air of coming in is by the piled bricks preheating of regenerator 20, and fuel from left to right sprays above the melten glass of the flame of gained in melting chamber 12 by the jet-burner 46 of left side spout 28 and the air mixed of preheating.In this stage of heating cycle, the burner nozzle in the right side spout 28 is not worked.Waste gas leaves melting chamber 12 and by one-level regenerator 22, the heat in the waste gas is passed to grid piled bricks 26 here by right side spout 28.In the embodiment shown in Fig. 1 and 2, the used heat by the regenerator system recoveries only has part to be finished by one-level regenerator 22.Other recovery of heat is finished by the secondary regenerator 36 in downstream.After the time of predetermined length, the burning of nozzle 46 commutation.More specifically, the burner nozzle in kiln 10 left sides is closed, and the right side nozzle is opened, and the combustion air of coming in is by right side regenerator 22, and waste gas leaves melting chamber 12 by the regenerator 20 in left side.
Still with reference to Fig. 1 and 2, represented a kind of NO of being used for
xThe layout of selective non-catalytic reduction.More specifically, in ammonia injected system 48 each flue 34 and 34 ＇ between each one-level regenerator and corresponding secondary regenerator.Though be not to be intended to limit the present invention, ammonia injected system 48 as shown in Figure 2 comprises by what a plurality of heat-stable materials were made and stretches into the pipe network that the pipe 52 in the flue 34 constitutes.Each pipe 52 communicates with collector 54, and collector 54 communicates with air-supply duct 56.Arrange a plurality of openings or spout to promote mixing fully of ammonia and whole exhaust flow by flue 34 along each pipe 52.In flue 34 ＇ of the opposite side of kiln 10, provide identical pipe net arrangement.In such glass melter, have been found that a part of discharge phase of waste gas in heating period by flue 34 is in preferred NO
xIn the reduction temperature scope, promptly 870～1090 ℃ (1598～1994 °F).As United States Patent (USP) 4,372,770 are proposed, and when ammonia mixes with hydrogen, this scope can expand 700～1090 ℃ (1292～1994 °F) to.The time that kiln waste gas keeps in this temperature range is depended on rate of heating, heating period, checker brick density and checker brick volume.
In the heating mode in the accompanying drawings, in the ammonia injected system 48 on right side, carry out the injection of ammonia, and left-sided system 48 ＇ close.In general, waste gas is discharged kiln 12 in the temperature of about 1537～1704 ℃ (2800～3100), enters regenerator., heat is passed to checker brick and be cooled when the regenerator at waste gas.After just heating commutation, the temperature of the waste gas of the flue 34 by waste gas one side generally is lower than ideal NO
xThe reduction scope, but in about 1～3 minute, be elevated to the ideal temperature range, this moment can begin the injection of ammonia.When the kiln spent air temperture in flue continues to raise, carry out the injection of ammonia continuously, surpass ideal NO up to its temperature
xDuring the reduction temperature scope, can stop the injection of ammonia.It should be understood, however, that to depend on rate of heating, heating period, checker brick density different with the checker brick volume, kiln waste gas may be in the temperature range that requires after just heating commutation.Under these circumstances, can be contemplated that said kiln waste gas will become Tai Re and can not inject reductive NO effectively by ammonia
x
Inject reductive NO by ammonia
xMethod may comprise some variations, for example, resemble United States Patent (USP) 3,900,554; 4,115,515; 4,328,020 and 4,372,770 proposed like that.
For further reductive NO
xDischarge, as United States Patent (USP) 4,372,770 proposed like that, can be incorporated into aftercombustion in the melting process.Aftercombustion is a kind ofly to be injected into fuel in the kiln waste gas and to make it by one-level regenerator 20 and a kind of method with the kiln waste-gas burning at 22 o'clock.Aftercombustion is used for reducing NO by the oxygen that consumes kiln waste gas
xFormation.Otherwise these oxygen may be used for NO
xFormation.Also the someone thinks that lacking oxygen causes NO in the kiln waste gas
xDecompose, the existence of ignitable fuel causes NO
xChemical reduction.All above-mentioned mechanism requires aftercombustion at NO
xCarry out under the temperature that may form.Someone thinks can obtain best result when fuel mixes in the temperature of 1420 ℃ (2600) with kiln waste gas at least.In the of the present invention specific embodiment shown in Fig. 2 and 3, fuel mixes with kiln waste gas in the upper end of one-level regenerator.More specifically, fuel arranged nozzle 58 makes it stretch into the neck of spout 28 from above.Make the angle of nozzle 58 relative with the exhaust flow direction, the injection speed of wishing fuel is that about 50～500 feet per seconds (STP) (15～150 metre per second (m/s)) are so that mix with kiln waste gas effectively.But the fuel that dotted line among Fig. 3 is represented injects nozzle 60 and 62 and has represented another kind of the relatively poor fuel injection phase of effect, is similar to point-blank in superposed pressure space 30 zones and with each spout 28.Can be fuel from mixing so that further strengthen with a plurality of nozzle ejections of each spout bonded.The injection of fuel also can be carried out in melting chamber before the outlet of spout.It should be understood that to there is no need to inject fuel, only make a part of spout have the aftercombustion ability and can obtain some advantages at each spout 28 places.In the multi-port kiln, different spouts have different rate of heating and different combustion/gas than being very common.So, in some cases, aftercombustion be limited to those have big rate of heating and/or in waste gas the spout of residual maximum surplus air may be the most effective.
The used fuel of aftercombustion can be any combustible hydrocarbon that is usually used in furnace fuel, most convenient be fuel of the same race used in the melting chamber 12, modal is Sweet natural gas (methane).The fuel quantity that injects is preferably near the amount of the required stoichiometric ratio of the oxygen completely consumed of the exhaust flow of injection place.From the maximum aftercombustion of the exhaust flow of kiln 10 require the usage quantity of postcombustion be up to melting chamber 12 consume 15% of fuel quantity, this depends on the excess air in the waste gas.When containing lower air capacity in the waste gas, need more a spot of fuel.This postcombustion can concentrate in the spout of several excess oxygen tolerance maximums, because as discussed above such, it is common the in service of glass melter that different spouts has different degree of oxidations.Those have, and the spout of high air/fuel ratio may form most NO
x, so aftercombustion should concentrate on waste gas one side of those spouts.
It should be understood that aftercombustion also can improve the temperature of kiln waste gas quickly, the feasible NO that is undertaken by ammonia injected system 48
xReduction in heating cycle, earlier begin.But, should also be understood that to have been found that aftercombustion has produced the raising of regenerator lattice brick temperature, for example about 40～45 ℃ (70～80 °F).So under the situation of support component near its ceiling temperature of checker brick, the amount of monitoring its temperature and limiting aftercombustion in view of the above needs.
Kiln waste gas is leaving one- level regenerator 20 and 22, and when entering distribution space 32, its temperature can change.For example, as discussed above, the temperature that escapes and enter the waste gas of allocation space from one- level regenerator 20 and 22 for some time after just commutating is lower than with ammonia injected system 48 carries out effective NO
xThe reductive preferred range.In addition, according to the length of each heating period, waste gas may reach the temperature that is higher than the ideal temperature scope makes ammonia injected system 48 can not remove NO effectively
xDischarge.In order to control the temperature of kiln waste gas when it flows through allocation space 32 and flue 34 arrival ammonia injected systems 48 in heating period, the present invention has utilized a surplus air burner 64.The surplus air burner be one the burner of the air mixed of fuel (for example, Sweet natural gas, oil or other combustible hydrocarbon polymer) and superfluous room temperature or preheating, promptly use than making the required stoichiometric air more air of said fuel combustion.The excess air that supplies to burner is used to control the heat that burner 64 produces.More specifically, when the waste gas of burner 64 mixed with kiln waste gas, the temperature of kiln waste gas will improve or reduce, thereby had changed the kiln spent air temperture in allocation space 32 and flue 34.By control fuel/air mixture ratio and burner 64 burnt fuel amounts, can control the temperature of kiln waste gas.If when waste gas passes through allocation space 32, have extra combustiblesubstance in the waste gas, surplus air burner 64 also can make its burning.
In the described particular of the present invention of Fig. 1, the bottom that burner 64 is arranged in one-level regenerator 22 walls 66 makes its waste gas directly enter allocation space 32.As a substitute scheme, can be along the space 32 arrange a plurality of burners.Controller 68 links to each other with burner 64 with control burner 64 burnt fuel amount and air capacities, thus the kiln spent air temperture in the control allocation space 32.The temperature of the kiln waste gas that temperature indicator 70 comes out with monitoring one- level regenerator 20 and 22 can be installed in space 32 and/or flue 34 if desired.This indicating meter 70 can link to each other with controller 68 with the fuel/air mixture of control burner 64, and the mixed airflow of guaranteeing kiln waste gas and burner gas is when its pipe network by ammonia injecting systems 48, and its temperature is in the effective needed temperature range of reduction kiln furnace exhaust.It should be understood that, when temperature monitor 70 is installed in the flue 34, before introducing the waste gas of surplus air burner to allocation space 32, the temperature of 70 monitorings of monitor kiln waste gas, and after the waste gas of introducing surplus air burner 64, the mixing temperature of temperature indicator 70 monitoring kiln waste gas and burner flue gas.If indicating meter 70 is installed within the regenerator piled bricks or the bottom, it will only monitor the temperature of kiln waste gas.
As a kind of replacement method of using surplus air burner 64,, optimize at ammonia injected system 48 NO of place in order to control the kiln spent air temperture
xReduction, can at kiln waste gas when the allocation space 32, atmosphere be injected in the kiln waste gas.But, preferably use the surplus air burner as mentioned above, because burner 64 can and provide better spent air temperture control in very wide temperature range internal combustion.
The surplus air burner 64 that this paper proposed reduces NO in two ways
xDischarge.At first, it has prolonged the time that ammonia injected system 48 is effectively moved by the temperature that changes kiln waste gas, and it is kept the longer time in the ideal temperature range of operation.More specifically, burner 64 can be lighted a fire providing temperature to be higher than the waste gas of kiln waste gas and unnecessary heat is provided, in the temperature of the early stage raising kiln waste gas of heating period.Burner 64 can also be lighted a fire to produce the waste gas that temperature is lower than the kiln spent air temperture, if desired, can reduce the kiln spent air temperture in the later stage of heating period.Secondly, if desired, burner 64 can be used for further controlling the kiln spent air temperture in narrower temperature range, makes that ammonia injected system 48 can be in its peak efficiencies operation.As previously discussed, preferably the temperature of waste gas still can be believed at 870～1090 ℃, if in 927～1010 ℃ temperature range kiln waste gas is sent into system 48, can improve the efficient of ammonia injected system 48.
Represented in this manual represented embodiment preferred, be understandable that, can make various variations and do not leave the determined scope of the present invention of following claims with the form of describing of the present invention.
Claims (19)
1, a kind of NO of feed glass melting process
xThe method of discharge, wherein, the fuel combustion in the melting furnaces has produced and has contained NO
xThe waste gas of compound, said kiln waste gas passes through a regenerator from said melting furnaces, arrive the downstream area of said regenerator, this method comprises the following steps: when said kiln waste gas is in predetermined temperature range, in said kiln waste gas, inject ammonia at said downstream area, to reduce NO
xThe content of compound, the temperature of the kiln waste gas in said downstream area is outside said predetermined temperature range the time, when flowing, to said kiln waste gas, introduces said downstream area other gas at said kiln waste gas from said regenerator, make that when kiln waste gas arrives said downstream area the mixing temperature of said kiln waste gas and said other gas is in said predetermined temperature range.
2, according to the process of claim 1 wherein, said gas is introduced the step that step is included in injecting gas under the certain temperature, makes that at said downstream area the mixing temperature of said kiln waste gas and said injecting gas is between about 870～1090 ℃.
3, according to the method for claim 2, wherein, said gas implantation step is included in the zone between said regenerator and the said downstream area, introduces step from the waste gas of at least one surplus air burner with the temperature that requires in said kiln waste gas.
4, according to the method for claim 3, wherein, when said kiln spent air temperture is lower than said predetermined temperature range, said burner gas temperature is higher than said kiln spent air temperture, when said kiln spent air temperture was higher than said predetermined temperature range, said burner flue gas temperature was lower than said kiln spent air temperture.
5, a kind of NO of feed glass melting process
xThe method of discharge, wherein, the fuel combustion in the melting furnaces has produced and has contained NO
xThe waste gas of compound, said kiln waste gas passes through a regenerator from said melting furnaces, arrive the downstream area of said regenerator, wherein, said kiln waste gas fluctuates in first temperature range in the temperature of said downstream area, this method comprises the following steps: when said kiln waste gas is in second temperature range, second temperature range within said first temperature range, in said kiln waste gas, inject ammonia at said downstream area, to reduce NO
xThe content of compound, when flowing, to said kiln waste gas, introduces said downstream area other gas to adjust said kiln spent air temperture at said kiln waste gas from said regenerator, make that when kiln waste gas arrives said downstream area the mixing temperature of said kiln waste gas and said other gas is in said second temperature range.
6, according to the method for claim 5, wherein, said other gas is introduced the step that step is included in injecting gas under the certain temperature, makes that at said downstream area the mixing temperature of said kiln waste gas and said injecting gas is between about 870～1090 ℃.
7, according to the method for claim 6, wherein, said gas is introduced the step that step is included in injecting gas under the certain temperature, makes that at said downstream area the mixing temperature of said kiln waste gas and said injecting gas is between about 927～1010 ℃.
8, according to the method for claim 6, wherein, said gas implantation step is included in the zone between said regenerator and the said downstream area, introduces step from the waste gas of at least one surplus air burner with the temperature that requires in said kiln waste gas.
9, method according to Claim 8, wherein, said burner flue gas is introduced step and is comprised said burner flue gas is incorporated into step in the allocation space under the said regenerator.
10, method according to Claim 8 also is included in the said ammonia implantation step hydrogen is injected into step in the said kiln waste gas.
11, method according to Claim 8, also comprise the following steps, promptly monitor said kiln spent air temperture and according to the said burner flue gas temperature of the corresponding adjustment of the variation of said kiln spent air temperture, make the mixing temperature of said kiln waste gas and said burner flue gas when arriving said downstream area in said second temperature range.
12, according to the method for claim 11, wherein, when said kiln spent air temperture is lower than said second temperature range, said burner gas temperature is higher than said kiln spent air temperture, when said kiln spent air temperture was higher than said second temperature range, said burner flue gas temperature was lower than said kiln spent air temperture.
13, according to the method for claim 11, also comprise when said kiln waste gas during from said regenerator to said downstream area, monitor the temperature of said kiln waste gas.
14, according to the method for claim 13, also be included in the introversive said kiln waste gas in a zone between said melting furnaces and the said regenerator and spray into the step of fuel, thereby consume oxygen in the said kiln waste gas by the burning of the said fuel that sprays into.
15, a kind of kiln of molten glass comprises:
A melting chamber;
A regenerator, wherein from the kiln waste gas of melting chamber by said regenerator, arrive the downstream area of said regenerator;
Be installed in the ammonia injector at said downstream area place, be used for when the said kiln waste gas that passes through said downstream area is in predetermined temperature range, spraying into ammonia with reductive NO
xCompound;
At the air injector of in said kiln waste gas, introducing the gas of preset temperature between said regenerator and the said downstream area, make that the mixing temperature of the gas of said kiln waste gas and said injection is in said predetermined temperature range at said downstream area place.
16, according to the kiln of claim 15, wherein, said air injector comprises at least one surplus air burner.
17,, also comprise an allocation space that is positioned under the said regenerator, and install in the kiln waste gas of said surplus air burner in said allocation space and introduce waste gas according to the kiln of claim 16.
18,, also comprise a temperature indicator, with monitoring kiln spent air temperture according to the kiln of claim 17.
19, according to the kiln of claim 17, also comprise when said kiln waste gas during by said regenerator, in said kiln waste gas, spray into the fuel injector of fuel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98107902A CN1203890A (en) | 1997-05-05 | 1998-05-04 | Reduction of Nox emissions in glass melting furnace |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US851,208 | 1997-05-05 | ||
| CN98107902A CN1203890A (en) | 1997-05-05 | 1998-05-04 | Reduction of Nox emissions in glass melting furnace |
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| Publication Number | Publication Date |
|---|---|
| CN1203890A true CN1203890A (en) | 1999-01-06 |
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ID=5219468
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98107902A Pending CN1203890A (en) | 1997-05-05 | 1998-05-04 | Reduction of Nox emissions in glass melting furnace |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102369165A (en) * | 2009-03-30 | 2012-03-07 | 琳德股份公司 | Cyclical stoichiometric variation of oxy-fuel burners in glass furnaces |
| CN101588995B (en) * | 2006-12-15 | 2012-08-29 | 法国燃气公司-苏伊士公司 | Glass melting oven |
| CN102762275A (en) * | 2009-11-26 | 2012-10-31 | 化学热处理技术股份有限公司 | Process and apparatus for cleaning offgases by means of regenerative thermal postcombustion |
| CN103803776A (en) * | 2014-02-22 | 2014-05-21 | 江苏中建材环保研究院有限公司 | SNCR (selective non-catalytic reduction) denitration device for flue gas in glass furnace |
| CN104524939A (en) * | 2014-12-12 | 2015-04-22 | 秦皇岛杰伯特环境科技有限公司 | Glass denitrification system based on SNCR technology |
| CN105797555A (en) * | 2016-03-31 | 2016-07-27 | 中国中轻国际工程有限公司 | Method for selective denitration through non-catalytic reduction method in glass melting furnace heat storage chamber |
| CN111278534A (en) * | 2017-10-31 | 2020-06-12 | 维特罗平板玻璃有限责任公司 | Emission reduction of Nitrogen Oxides (NOX) in oxygen combustion furnaces |
-
1998
- 1998-05-04 CN CN98107902A patent/CN1203890A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101588995B (en) * | 2006-12-15 | 2012-08-29 | 法国燃气公司-苏伊士公司 | Glass melting oven |
| CN102369165A (en) * | 2009-03-30 | 2012-03-07 | 琳德股份公司 | Cyclical stoichiometric variation of oxy-fuel burners in glass furnaces |
| CN102762275A (en) * | 2009-11-26 | 2012-10-31 | 化学热处理技术股份有限公司 | Process and apparatus for cleaning offgases by means of regenerative thermal postcombustion |
| CN102762275B (en) * | 2009-11-26 | 2015-06-10 | 化学热处理技术股份有限公司 | Process and apparatus for cleaning offgases by means of regenerative thermal postcombustion |
| CN103803776A (en) * | 2014-02-22 | 2014-05-21 | 江苏中建材环保研究院有限公司 | SNCR (selective non-catalytic reduction) denitration device for flue gas in glass furnace |
| CN104524939A (en) * | 2014-12-12 | 2015-04-22 | 秦皇岛杰伯特环境科技有限公司 | Glass denitrification system based on SNCR technology |
| CN105797555A (en) * | 2016-03-31 | 2016-07-27 | 中国中轻国际工程有限公司 | Method for selective denitration through non-catalytic reduction method in glass melting furnace heat storage chamber |
| CN111278534A (en) * | 2017-10-31 | 2020-06-12 | 维特罗平板玻璃有限责任公司 | Emission reduction of Nitrogen Oxides (NOX) in oxygen combustion furnaces |
| CN111278534B (en) * | 2017-10-31 | 2022-07-15 | 维特罗平板玻璃有限责任公司 | Emission reduction of Nitrogen Oxides (NOX) in oxygen combustion furnaces |
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